[go: up one dir, main page]
More Web Proxy on the site http://driver.im/

US7081312B1 - Multiple stage combustion process to maintain a controllable reformation temperature profile - Google Patents

Multiple stage combustion process to maintain a controllable reformation temperature profile Download PDF

Info

Publication number
US7081312B1
US7081312B1 US09/669,969 US66996900A US7081312B1 US 7081312 B1 US7081312 B1 US 7081312B1 US 66996900 A US66996900 A US 66996900A US 7081312 B1 US7081312 B1 US 7081312B1
Authority
US
United States
Prior art keywords
fuel cell
fuel
reaction
endothermic
exothermic
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime, expires
Application number
US09/669,969
Inventor
William Henry Pettit
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
GM Global Technology Operations LLC
Original Assignee
General Motors Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by General Motors Corp filed Critical General Motors Corp
Assigned to GENERAL MOTORS CORPORATION reassignment GENERAL MOTORS CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: PETTIT, WILLIAM HENRY
Priority to US09/669,969 priority Critical patent/US7081312B1/en
Priority to DE10147368A priority patent/DE10147368A1/en
Priority to JP2001294237A priority patent/JP2002198074A/en
Priority to US10/962,802 priority patent/US7842424B2/en
Priority to US10/962,651 priority patent/US7993784B2/en
Publication of US7081312B1 publication Critical patent/US7081312B1/en
Application granted granted Critical
Assigned to GM GLOBAL TECHNOLOGY OPERATIONS, INC. reassignment GM GLOBAL TECHNOLOGY OPERATIONS, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: GENERAL MOTORS CORPORATION
Assigned to UNITED STATES DEPARTMENT OF THE TREASURY reassignment UNITED STATES DEPARTMENT OF THE TREASURY SECURITY AGREEMENT Assignors: GM GLOBAL TECHNOLOGY OPERATIONS, INC.
Assigned to CITICORP USA, INC. AS AGENT FOR HEDGE PRIORITY SECURED PARTIES, CITICORP USA, INC. AS AGENT FOR BANK PRIORITY SECURED PARTIES reassignment CITICORP USA, INC. AS AGENT FOR HEDGE PRIORITY SECURED PARTIES SECURITY AGREEMENT Assignors: GM GLOBAL TECHNOLOGY OPERATIONS, INC.
Assigned to GM GLOBAL TECHNOLOGY OPERATIONS, INC. reassignment GM GLOBAL TECHNOLOGY OPERATIONS, INC. RELEASE BY SECURED PARTY Assignors: UNITED STATES DEPARTMENT OF THE TREASURY
Assigned to GM GLOBAL TECHNOLOGY OPERATIONS, INC. reassignment GM GLOBAL TECHNOLOGY OPERATIONS, INC. RELEASE BY SECURED PARTY (SEE DOCUMENT FOR DETAILS). Assignors: CITICORP USA, INC. AS AGENT FOR BANK PRIORITY SECURED PARTIES, CITICORP USA, INC. AS AGENT FOR HEDGE PRIORITY SECURED PARTIES
Assigned to UNITED STATES DEPARTMENT OF THE TREASURY reassignment UNITED STATES DEPARTMENT OF THE TREASURY SECURITY AGREEMENT Assignors: GM GLOBAL TECHNOLOGY OPERATIONS, INC.
Assigned to UAW RETIREE MEDICAL BENEFITS TRUST reassignment UAW RETIREE MEDICAL BENEFITS TRUST SECURITY AGREEMENT Assignors: GM GLOBAL TECHNOLOGY OPERATIONS, INC.
Assigned to GM GLOBAL TECHNOLOGY OPERATIONS, INC. reassignment GM GLOBAL TECHNOLOGY OPERATIONS, INC. RELEASE BY SECURED PARTY (SEE DOCUMENT FOR DETAILS). Assignors: UAW RETIREE MEDICAL BENEFITS TRUST
Assigned to GM GLOBAL TECHNOLOGY OPERATIONS, INC. reassignment GM GLOBAL TECHNOLOGY OPERATIONS, INC. RELEASE BY SECURED PARTY (SEE DOCUMENT FOR DETAILS). Assignors: UNITED STATES DEPARTMENT OF THE TREASURY
Assigned to WILMINGTON TRUST COMPANY reassignment WILMINGTON TRUST COMPANY SECURITY AGREEMENT Assignors: GM GLOBAL TECHNOLOGY OPERATIONS, INC.
Assigned to GM Global Technology Operations LLC reassignment GM Global Technology Operations LLC CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). Assignors: GM GLOBAL TECHNOLOGY OPERATIONS, INC.
Assigned to GM Global Technology Operations LLC reassignment GM Global Technology Operations LLC RELEASE BY SECURED PARTY (SEE DOCUMENT FOR DETAILS). Assignors: WILMINGTON TRUST COMPANY
Adjusted expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/248—Reactors comprising multiple separated flow channels
    • B01J19/249—Plate-type reactors
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C01B3/58—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction
    • C01B3/583—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction the reaction being the selective oxidation of carbon monoxide
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/02—Details
    • H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
    • H01M8/0258—Collectors; Separators, e.g. bipolar separators; Interconnectors characterised by the configuration of channels, e.g. by the flow field of the reactant or coolant
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of reactants
    • H01M8/04022—Heating by combustion
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04223—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids during start-up or shut-down; Depolarisation or activation, e.g. purging; Means for short-circuiting defective fuel cells
    • H01M8/04225—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids during start-up or shut-down; Depolarisation or activation, e.g. purging; Means for short-circuiting defective fuel cells during start-up
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
    • H01M8/241—Grouping of fuel cells, e.g. stacking of fuel cells with solid or matrix-supported electrolytes
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
    • H01M8/2457—Grouping of fuel cells, e.g. stacking of fuel cells with both reactants being gaseous or vaporised
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
    • H01M8/2465—Details of groupings of fuel cells
    • H01M8/2484—Details of groupings of fuel cells characterised by external manifolds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2451—Geometry of the reactor
    • B01J2219/2453—Plates arranged in parallel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2451—Geometry of the reactor
    • B01J2219/2456—Geometry of the plates
    • B01J2219/2458—Flat plates, i.e. plates which are not corrugated or otherwise structured, e.g. plates with cylindrical shape
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2461—Heat exchange aspects
    • B01J2219/2462—Heat exchange aspects the reactants being in indirect heat exchange with a non reacting heat exchange medium
    • B01J2219/2464—Independent temperature control in various sections of the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2461—Heat exchange aspects
    • B01J2219/2465—Two reactions in indirect heat exchange with each other
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2469—Feeding means
    • B01J2219/247—Feeding means for the reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2477—Construction materials of the catalysts
    • B01J2219/2479—Catalysts coated on the surface of plates or inserts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2477—Construction materials of the catalysts
    • B01J2219/2481—Catalysts in granular from between plates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2483—Construction materials of the plates
    • B01J2219/2485—Metals or alloys
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2483—Construction materials of the plates
    • B01J2219/2487—Ceramics
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2491—Other constructional details
    • B01J2219/2492—Assembling means
    • B01J2219/2496—Means for assembling modules together, e.g. casings, holders, fluidic connectors
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0435—Catalytic purification
    • C01B2203/044—Selective oxidation of carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/066—Integration with other chemical processes with fuel cells
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0822—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel the fuel containing hydrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0827—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel at least part of the fuel being a recycle stream
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1005—Arrangement or shape of catalyst
    • C01B2203/1029—Catalysts in the form of a foam
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1217—Alcohols
    • C01B2203/1223—Methanol
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1288—Evaporation of one or more of the different feed components
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/1614—Controlling the temperature
    • C01B2203/1619—Measuring the temperature
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/1642—Controlling the product
    • C01B2203/1671—Controlling the composition of the product
    • C01B2203/1676—Measuring the composition of the product
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/1695—Adjusting the feed of the combustion
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • This invention relates to fuel cell systems and components, and more particularly to a fuel cell system that combines exothermic and endothermic processes in one reaction vessel.
  • a primary advantage of fuel cells is that fuel cells can convert stored energy to electricity with about 60–70 percent efficiency, with higher efficiencies theoretically possible. Further, fuel cells produce virtually no pollution. These advantages make fuel cells particularly suitable for vehicle propulsion applications and to replace the internal combustion engine which operates at less than 30 percent efficiency and can produce undesirable emissions.
  • a fuel cell principally operates by oxidizing an element, compound or molecule (that is, chemically combining with oxygen) to release electrical and thermal energy.
  • fuel cells operate by the simple chemical reaction between two materials such as a fuel and an oxidant.
  • hydrogen is consumed by reacting the hydrogen with oxygen from air to produce water, electrical energy and heat. This is accomplished by feeding the hydrogen over a first electrode (anode), and feeding the oxygen over a second electrode (cathode).
  • the two electrodes are separated by an electrolyte which is a material that allows charged molecules or “ions” to move through the electrolyte.
  • electrolytes There are several different types of electrolytes that can be utilized including the acid-type, alkaline-type, molten-carbonate-type and solid-oxide-type.
  • PEM proto exchange membrane electrolytes
  • solid polymer electrolyte are of the acid-type, and potentially have high-power and low-voltage, and thus are desirable for vehicle applications.
  • FIG. 1 shows a fuel cell that has been simplified for purposes of illustrating the operation of a fuel cell.
  • a hydrogen gas stream 12 is fed into a first sealed chamber or manifold (in the case of a fuel cell stack) 14 and over a first electrode (anode) 24 and on to a first face 16 (the anode side) of a proton exchange membrane assembly assembly 18 .
  • the proton exchange membrane assembly 18 typically includes the electrolyte membrane 19 having two faces, and on each face there is a catalyst, usually a noble metal such as platinum, and an electrically conductive diffusion media (such as a carbon fiber mat) overlying the catalyst.
  • the catalyst and diffusion media are not shown in FIG. 1 .
  • the catalyst on the anode face of the assembly promotes the dissociation of hydrogen molecules and the catalyst on the cathode face of the assembly promotes the dissociation of oxygen molecules and a reaction of oxygen with hydrogen protons to produce water.
  • the electrolyte membrane 19 allows the diffusion of hydrogen ions 26 from one electrode 24 to another electrode 34 .
  • FIG. 1 is a simple illustration attempting to depict the diffusion of these hydrogen ions 26 from the anode to the cathode side of the electrolyte membrane. However, the electrolyte membrane 19 does not include channels as shown in FIG. 1 .
  • a compressed air stream 22 is supplied to a second chamber or manifold (for a fuel cell stack) 15 in a manner so that the compressed air flows over a second electrode (cathode) 34 and on to a second face 20 of the proton exchange membrane assembly 18 .
  • the proton exchange membrane assembly 18 is selective and allows only the hydrogen protons 26 to pass through the membrane assembly 18 rejecting larger diatomic hydrogen molecules 28 .
  • a single hydrogen proton (or its equivalent) 26 passes through the membrane, it leaves behind an electron 30 .
  • the electrons 30 that are left behind can be collected in the electrode (conductor) 24 .
  • fuel cell systems include a stack of single cells (fuel cell stack) with adjacent cells sharing a common electrode. In that case, the electrodes 24 , 34 would be bipolar.
  • each electrode 24 , 34 includes channels 25 formed therein through which either hydrogen or oxygen flows.
  • the concentrated electrons in the electrode 24 causes a potential negative voltage on the electrode 24 due to the excess of electrons (because the electrons are negatively charged).
  • the oxygen molecules are directed to the second face 20 of the proton exchange membrane assembly 18 , the oxygen meets the hydrogen proton 26 as the proton passes through the membrane.
  • the chemical reaction of the hydrogen proton 26 and the oxygen on the cathode side of the cell requires electrons and therefore a shortage of electrons is created.
  • the needed electrons can be supplied by a second electrode 34 (that is, the cathode electrode).
  • the oxygen and the hydrogen proton 26 in the presence of the electrons 30 from the second electrode 34 , easily combined to produce water 32 .
  • the reactions at the electrodes are as follows: Anode 2H 2 ⁇ 4H + +4e ⁇ Cathode O 2 +4e ⁇ +4H + ⁇ 2H 2 O.
  • an electrical potential exists between the two electrodes. That is, the hydrogen electrode 24 has an excess of electrons and the oxygen electrode 34 needs electrons.
  • the electrical potential can be utilized by placing an electrical load, such as electrical motor 36 (to propel a vehicle) between the anode 24 and the cathode 34 . Since electrical energy is used as it goes around the loop, the only by-products of this fuel system are water vapor and the heat loss through inefficiency of the cell itself (or about 30 percent of the power). With 70 percent efficiency, this process is significantly more attractive for extracting stored energy than an internal combustion engine that typically extracts only 20–30 percent of stored fuel energy.
  • Both hydrogen and oxygen are each supplied to the fuel cell in excess to provide the greatest rate of reaction possible.
  • the hydrogen gas stream will be under pressure of about 3 bars if it is produced from a fuel reformation reaction and therefore the oxygen stream 22 must be pumped up to the same pressure to avoid damage to the proton exchange membrane and the catalyst of the assembly 18 .
  • Any water produced or remaining on either side of the fuel cell is removed and is discharged or may be sent through a water/vapor stream line 38 to a water reservoir (such as the holding tank 46 shown in FIG. 2 ) for use in other components or for use in the fuel cell at startup.
  • tail gas exhaust stream 40 , 42 from both sides of the fuel cell are discharged to the atmosphere or preferably are supplied to a combustor for burning and producing heat needed for other operations such as the fuel reformation process described hereafter. Since the reactants are supplied to the fuel cell in excess, tail gas exhaust stream 40 from the anode side contains hydrogen and the tail gas exhaust stream 42 from the cathode side contains oxygen. Both of the fuel cell tail gas streams 40 , 42 may be combusted in a catalytic combustor to provide heat for other components in the fuel cell system.
  • the fuel cell is maintained at a temperature of about 80 degrees Celsius or greater. Maintaining this temperature may require heat to be added or removed from the fuel cell stack. Often heat must be supplied to the fuel cell at startup. This heat can be supplied by a catalytic or flame combustor. However, during post startup or normal operation of the fuel cell, heat is generated by the fuel cell and the generated heat can be removed by any of a variety of heat exchange methods but preferably is removed using a liquid coolant.
  • fuel cell systems require a variety of auxiliary equipment such as pumps, heat exchangers, fuel processors, combustors, water separation and collection equipment, hydrogen cleanup or purification systems and so on to support the operation of the fuel cell itself.
  • auxiliary equipment such as pumps, heat exchangers, fuel processors, combustors, water separation and collection equipment, hydrogen cleanup or purification systems and so on.
  • compressed or liquefied hydrogen could be used to operate a fuel cell in a vehicle, to date this is not practical.
  • the use of compressed or liquefied hydrogen ignores the extensive infrastructure currently being used to supplying gasoline for internal combustion engine automobiles and trucks. Consequently, it is more desirable to utilize a fuel such as methanol, gasoline, diesel, methane and the like to provide a hydrogen source for the fuel cell.
  • a fuel such as methanol, gasoline, diesel, methane and the like
  • the methanol, gasoline, diesel, methane and the like must be reformed to provide a hydrogen gas source. This is accomplished by using methanol or gasoline fuel processing or reforming equipment, and hydrogen cleanup or purification equipment.
  • Fuel cell systems often include a fuel processing section which reforms the fuel such as methanol, gasoline, diesel, methane and the like to produce hydrogen and a variety of other byproducts.
  • a fuel processing section which reforms the fuel such as methanol, gasoline, diesel, methane and the like to produce hydrogen and a variety of other byproducts.
  • these reforming (reformation) processes are endothermic and require energy input to drive the reformation reaction.
  • a catalytic or flame combustor is utilized to provide heat for the reforming process. Most often, this is accomplished by utilizing a working fluid (liquid or gas) loop that transfers heat from the combustion process to the reforming process.
  • a working fluid loop that transfers heat from the combustion process to the reforming process.
  • the response time for heat transfer needed during startup and transient conditions of the fuel cell are less than optimal when the system uses a fluid to transfer heat between the combustor and the reformer vessel.
  • the working fluid loop, associated heat exchangers and piping add to the overall mass and volume of the fuel cell system.
  • the invention includes a reaction vessel that integrates and balances an endothermic process with at least one exothermic process of a fuel cell system.
  • the exothermic process is conducted in stages to provide more uniform and/or controllable heat generation and exchange, and to produce a uniform, and/or controllable temperature profile in the endothermic reaction process, if desired (depending on the fuel used).
  • the invention eliminates the working fluid heat exchange loop of prior art fuel reforming sections that had unsatisfactory response times at startup, and during transient conditions, and also added to the overall mass and volume of the fuel cell system.
  • One embodiment of the invention includes a reaction vessel having an outer shell and catalyst carried in the shell for promoting an endothermic reaction.
  • the reaction vessel is constructed and arranged to charge an endothermic reactant(s) into the shell.
  • a plurality of heat exchanger devices are also provided having portions separately positioned and carried within the shell. Each heat exchanger device is independently controlled from the other heat exchanger devices so that heat transferred by the heat exchanger devices to the catalyst, and the temperature of the catalyst in the shell, may be varied at different locations within the reaction vessel.
  • the reaction vessel is constructed and arranged so that exothermic reactants may be charged into each heat exchanger device and combusted to generate heat for driving the endothermic reaction occurring in another portion of the reaction vessel.
  • the exothermic reactants may include anode and cathode exhaust streams from a fuel cell stack.
  • Another embodiment of the present invention includes a reaction vessel having a plurality of endothermic reaction sections and a plurality of heat transfer devices.
  • Each heat transfer device is associated with an endothermic reaction section so that sufficient heat may be transferred to the endothermic reaction section and so as to control the temperature profile of the endothermic reaction section within a predetermined range.
  • the endothermic reaction sections may be spaced apart from each other and so that a heat transfer device is positioned between adjacent spaced apart endothermic reaction sections.
  • Another embodiment of the present invention includes a combination reaction vessel having multiple staged catalytic combustion chambers and a plurality of endothermic reaction chambers.
  • Each endothermic reaction chamber has a combustion chamber adjacent thereto so that heat generated in the combustion chamber is transferred to the adjacent endothermic reaction chamber.
  • Each catalytic combustion chamber may have a plurality of reactant charge openings for supplying at least one reactant to the catalytic combustion chamber. The charge openings may be positioned within the catalytic combustion chamber to provide a substantially uniform temperature along the length of the catalytic combustion chamber.
  • Another embodiment of the invention includes a charge manifold having a plurality of charge pipes extending therefrom.
  • Each charge pipe extends into an exothermic reaction chamber.
  • the charge pipes have charge holes provided along the length of each charge pipe so the fuel or oxidant may be charged into the combustion reaction chamber through the charge holes.
  • Preferably valves are associated with each charge pipe and a controller is provided for selectively controlling the amount of fuel or oxidant charged to each exothermic reaction chamber.
  • Each charge pipe may separate adjacent side-by-side exothermic reaction chambers.
  • a directional flow header may be provided at the end of each exothermic reaction chamber for directing gases exiting one exothermic reaction chamber to the entrance of an adjacent side-by-side exothermic reaction chamber.
  • Another embodiment of present invention includes the incorporation of a fuel/water vaporizer into the combination reaction vessel.
  • a fuel/water mixture is injected into a plurality of vaporization chambers and is vaporized by heat generated by the catalytic combustion of a fuel mixture charged into a plurality of exothermic reaction chambers.
  • No catalyst is provided in the vaporization chambers.
  • An oxidant and fuel are charged into the exothermic reaction chambers and catalytically combusted to produce heat to vaporize the fuel/water mixture.
  • Another embodiment of present invention includes a combination reaction vessel that incorporates an exothermic and endothermic reaction.
  • the reaction vessel includes a plurality of endothermic reaction chamber sections that are spaced apart vertically and horizontally.
  • a plurality of exothermic reaction chamber sections are also provided in a spaced apart fashion so that a partition section is provided between laterally spaced apart exothermic reaction chamber sections.
  • the partition sections provide for staged adiabatic reforming of the fuel/water mixture.
  • the catalyst loading in different portions of the endothermic reaction chamber sections may be varied as desired.
  • FIG. 1 illustrates a fuel cell useful in the present invention
  • FIG. 2 is a schematic illustration of a fuel cell system useful in a present invention
  • FIG. 3 is a sectional view of a combination reaction vessel for housing an endothermic and an exothermic reaction according to the present invention
  • FIG. 4 is a sectional view of an alternative embodiment of a combination reaction vessel for housing an endothermic and an exothermic reaction according to the present invention
  • FIG. 5 is a sectional view of an alternative embodiment of a combination reaction vessel for housing an endothermic and an exothermic reaction according to the present invention
  • FIG. 6 is an exploded, prospective view, with portions broken away, of an alternative embodiment of a combination reaction vessel for housing an endothermic and an exothermic reaction according to the present invention.
  • FIG. 7 is a sectional view of an alternative embodiment of a reaction vessel for housing a staged endothermic reaction according to the present invention.
  • the fuel cell system includes a fuel cell (or fuel cell stack) 10 .
  • the system may also include the following auxiliary equipment to support the fuel cell stack 10 .
  • Water is provided and held in a water reservoir or holding tank 46 which is connected to a vaporizer 48 by water line 44 .
  • a fuel source is provided and held in a tank 52 that is also connected to the vaporizer 48 by line 50 .
  • the fuel used is methanol, gasoline, diesel, methane and the like.
  • the fuel and water may be vaporized by any method known to those skilled in the art, but preferably the heat for the vaporization step is supplied by a heat exchanger 39 in the vaporizer that catalytically combusts hydrogen 40 ′ and oxygen 42 ′ from the fuel cell stack 10 exhaust.
  • the vaporizer may be included as an integral part of the reaction vessel 54 as will be described hereafter.
  • the fuel and water are vaporized together (or may be vaporized separately) and a resultant vaporized fuel/water stream is delivered via line 58 to an endothermic reaction section of a combination reaction vessel 54 .
  • a fuel reformation process is conducted in the endothermic reaction section.
  • the combination reaction vessel 54 also houses an exothermic reaction section.
  • the exothermic reaction may be, for example, catalytic combustion of a fuel or preferential oxidation of the exhaust stream from the fuel reforming section. If the exothermic reaction process is catalytic combustion, preferably the anode exhaust stream 40 and cathode exhaust stream 42 from the fuel cell 10 are used as the catalytic combustion reactants.
  • the exhaust from the exothermic reaction may be discharged to the atmosphere via line 43 .
  • the reformation process effluent stream 56 may include hydrogen molecules (H 2 ), CO, CO 2 , N 2 , CH 4 .
  • the reformation process effluent stream 56 may be delivered to a hydrogen purification section 59 to reduce the concentration of CO and hydrocarbons (or carbon based molecules).
  • the hydrogen purification section 59 may include any of a variety of components for purifying the reformation process effluent stream 56 and may include high and low temperature reactors to shift the equilibrium of the stream 56 constituents (thus reducing the concentration of CO), preferential oxidation reactor(s), additional hydrocarbon reforming components, separators, adsorbers and similar equipment.
  • Eventually a hydrogen rich stream 60 is delivered to the anode side of the fuel cell 10 .
  • air 22 is pumped to the cathode side of the fuel cell 10 .
  • the anode and cathode exhaust streams from the fuel cell stack carry water that can be condensed out using a separator/condenser as the stream exits fuel cell stack and the liquid water may be sent to reservoir 46 .
  • the water may be condensed out after the stack effluent passes through exhaust tail gas combustors.
  • FIG. 3 illustrates a combination reaction vessel 54 for housing an endothermic and an exothermic reaction.
  • the combination reaction vessel 54 includes an endothermic reaction chamber section 62 and an exothermic reaction chamber section 64 that share a common wall or substrate 66 .
  • Each endothermic reaction chamber section 62 and exothermic reaction chamber section 64 includes an associated outside wall 68 , 70 respectively.
  • a catalyst 61 for promoting the reformation reaction of the fuel and water, is provided in the endothermic reaction chamber section 62 . As illustrated in FIG. 3 the catalyst 61 may overlie at least one of the outside wall 68 and/or the substrate 66 .
  • the catalyst 61 may be provided directly on the outside wall 68 or the substrate 66 , or intermediate layers (not shown) may be provided therebetween.
  • the vaporized fuel and water mixture may enter the endothermic reaction chamber section 62 from one end 72 or may be selectively charged to the endothermic reaction chamber through charge lines 74 or openings 75 selectively positioned along the length of the endothermic reaction chamber section 62 .
  • endothermic reactants as used herein means reactants of an endothermic reaction. In this case, for example, the endothermic reactants are the organic fuel and water.
  • the exothermic reaction chamber section 64 may be similarly constructed. As illustrated in FIG. 3 , an exothermic catalyst 65 may overlie at least one of the outside wall 70 or substrate 66 . Similarly, the catalyst 65 may be provided directly on the outside wall 70 or the substrate 66 , or intermediate layers (not shown) may be provided therebetween.
  • a fuel combustion process may be conducted in the exothermic reaction chamber 64 .
  • An oxidant such as oxygen (from air) may be charged into the chamber section 64 through one end 76 of the chamber and a fuel such as hydrogen or a hydrocarbon may be supplied to the chamber through one or more charge lines 74 ′ or through a charge openings 75 ′ that may be positioned along the length of the exothermic reaction chamber section 64 .
  • the fuel may be charged through the open end 76 and the oxidant supplied through the charge lines 74 ′ or charge openings 75 ′.
  • an exothermic reaction such as a preferential oxidation reaction to reduce CO or hydrocarbons may be conducted in the exothermic reaction chamber section 64 .
  • the heat generated by the exothermic reaction in the exothermic reaction chamber section 64 is transferred through the substrate 66 to warm the endothermic reaction chamber section 62 , catalyst 61 and reactants, and to drive (that is, to provide the heat necessary to complete the reaction) the endothermic reaction process.
  • the term “exothermic reactants” as used herein means the reactants of an exothermic reaction.
  • the exothermic reactants may include a fuel such as an organic fuel including, for example, hydrogen, methanol, gasoline, diesel, methane and the like; and an oxidant, such as oxygen in the form of air.
  • FIG. 4 illustrates an alternative embodiment of the present invention wherein either the endothermic or the exothermic catalyst may be provided on a solid porous substrate 78 or porous pellets 80 or any of a variety materials that would provide increased surface area for either of the catalysts.
  • the catalyst is also considered to be overlying the substrate for purposes of this invention.
  • FIG. 5 illustrates an alternative embodiment of the present invention wherein a reactant charge pipe 82 extends into one of the reaction chambers 62 , 64 and has a plurality of discharge holes 84 formed therein along the length of the reaction chamber to selectively discharge a reactant into the chamber at predetermined locations.
  • the charge pipe 82 delivers a fuel such as hydrogen to the combustion reaction chamber 64 which has an oxidant such as oxygen or air flowing therein.
  • the charge pipe 82 may be used to introduce oxygen to allow for staged preferential oxidation.
  • reactant charge pipe 82 with discharge holes 84 allows the fuel or oxidant to be supplied in relatively low concentrations so as to reduce the risk of autoignition and also to provide a more uniform heat generation profile along the length of the exothermic reaction chamber 64 .
  • porous catalyst pellets or another suitable supported catalyst may be provided in the exothermic reaction chamber 64 .
  • the substrate 66 may be made from a variety of materials having suitable heat transfer characteristics and may include any of several metals such as stainless-steel, copper, aluminum, or any of a variety of composites, ceramics, compounds or polymer base materials.
  • the combination reaction vessel provides a staged exothermic reaction process (preferably combustion of a fuel) to provide a uniform temperature profile and heat transfer to drive an endothermic reaction (preferably a fuel reforming process) occurring in an adjacent chamber.
  • another embodiment of the present invention includes a combination reaction vessel 54 having a plurality of spaced apart, parallel endothermic reaction chambers 62 .
  • the endothermic reaction chambers 62 are vertically spaced apart and separated by an exothermic reaction chamber 64 that has a longitudinal axis and flow path running in a perpendicular direction to the longitudinal axis and flow path of the endothermic reaction chamber 62 .
  • parallel co-flowing and counter flow configurations are contemplated as a part of the present invention.
  • an endothermic reaction catalyst is provided in each of the endothermic reaction chambers 62 and the endothermic reactants, such as a methanol/water, gasoline/water vapor mixture, or other fuel/water mixture are supplied through one end 72 (see also FIG. 3 ) of the endothermic reaction chamber and flow in the direction indicated by arrow shown entering the reaction chamber 62 in FIG. 6 .
  • the endothermic reactants such as a methanol/water, gasoline/water vapor mixture, or other fuel/water mixture
  • a plurality of spaced apart parallel exothermic reaction chambers 64 are provided so that each exothermic chamber 64 separates two endothermic reaction chambers 62 so as to provide a staged exothermic reaction process.
  • the exothermic chambers 64 may also be arranged in a laterally adjacent side-by-side configuration.
  • An inlet header 86 is provided having an inlet opening 88 formed therein through which at least one of the exothermic reactants is charged to the exothermic reaction chambers 64 .
  • exhaust gas (which contains oxygen) from the cathode side of the fuel cell is feed through the inlet opening 88 .
  • the cathode exhaust gas flows down a first set of exothermic reaction chambers and is directed by a flow directing header 90 down a second set of exothermic reaction chambers, and so on in a serpentine fashion throughout the combination reaction vessel 54 and finally exits through an exhaust opening 92 formed in an outlet header 94 .
  • a second exothermic reaction reactant may be charged into the exothermic reaction chambers 64 utilizing a charge manifold 96 .
  • the charge manifold 96 includes a plurality of charge pipes or lines 82 .
  • a charge pipe 82 is received in one of each of the exothermic reaction chambers 64 .
  • the charge pipe 82 has a plurality of discharge holes 84 which are spaced apart along the length of the exothermic reaction chamber (as also shown in FIG. 5 ).
  • the combination reaction vessel 54 may be constructed and arranged so that the charge pipes 82 also function to separate laterally adjacent side-by-side exothermic reaction chambers. That is, the charge crepe 82 acts as a wall separating laterally adjacent exothermic reaction chambers.
  • the heat generated throughout the exothermic reaction chamber may be controlled so that it is substantially uniform, or graduated is so desired. Consequently, the heat transferred to the endothermic reaction chamber, catalyst and reactants is such that the temperature profile in the endothermic reaction chamber is controlled to be substantially uniform, or graduated if so desired. Maintaining a controllable temperature profile in a fuel reforming process is important to avoid undesirable side effects such as catalyst degradation, or methane slip. At low power, the temperature profile may be such as to promote a high temperature reformation with a high temperature shift reaction at the exit of the reaction chamber. The temperature at the exit end of the reaction chamber should be high enough to suppress methane formation for a given catalyst.
  • a plurality of temperature or concentrations sensors 104 may be selectively placed in the combination reaction vessel, and valves 100 may be included in the charge manifold 96 to selectively control the amount of reactant being charged to the chamber and thus control the reaction as desired.
  • Associated on-board computer controllers 102 , drivers and associated electrical equipment can be provided to control the above described components and processes in a manner known to those skilled in the art.
  • the charge manifold 96 may be constructed and arranged to controllably charge reactants so that a uniform temperature profile at full power is provided which would utilize the entire reactor volume.
  • the charge manifold 96 may be constructed and arranged to controllably charge reactants so that a uniform temperature profile at full power is provided which would utilize the entire reactor volume.
  • turndown situations for example, when the vehicle is stopped
  • less power is require, and thus only a portion of the reactor is required to reform fuel because of the lower power demand.
  • the remaining endothermic reaction sections or portions thereof could be utilized to perform a water gas shift reaction to reduce the concentration of CO in the fuel reforming stream.
  • the temperature in the first two endothermic reaction sections could be controlled to provide relatively high temperature fuel reforming and the temperature in the remaining endothermic reaction sections (that is, in the rearward portion of the reaction vessel) could be controlled to be relatively low thereby reducing unwanted reformation byproducts and so that a maximum conversion is accomplished during the fuel reforming while minimizing methane slip.
  • the vaporizer may be included in the front portion of the combination reaction vessel 54 .
  • the combination reaction vessel shown in FIG. 7 operates similarly to the vessel shown in FIG. 2 , but with a few exceptions.
  • a fuel/water mixture may be charge through line 258 into a first section of the combination reaction vessel 54 to be vaporized in a first heat exchanger section 202 .
  • the fuel/water mixture flows through a plurality of spaced apart chamber 262 ′ that do not include a fuel reforming catalyst. Thereafter, the endothermic reaction chambers 262 include a fuel reforming catalyst as previously discussed.
  • the fuel/water mixture entering the chambers 262 ′ is vaporized by heat generated by the catalytic combustion of a combustion fuel mixture charged into a plurality of exothermic reaction chambers 264 .
  • An oxidant or fuel preferably an oxidant such as oxygen from the fuel cell stack effluent, may be charged to the exothermic reaction chambers 264 through a charge line 242 and header 243 .
  • An oxidant or fuel preferably a fuel such as hydrogen from the fuel cell stack effluent, is charged to the exothermic reaction chambers 264 through charge line 282 .
  • a combustion fuel mixture travels through the plurality of spaced apart exothermic reaction chambers 264 generating heat to vaporize the fuel/water mixture or reform the fuel/water mixture.
  • one of the oxidant or fuel is charged to the exothermic reaction chambers 264 through charge lines 282 in a staged fashion as previously discussed.
  • the exothermic reaction chambers 264 to are spaced apart vertically and horizontally so that a partition section 299 is provided between laterally spaced apart exothermic reaction chambers 264 .
  • the partition sections 299 provide for staged adiabatic reformation of the fuel/water mixture.
  • the catalyst loading in different portions of the endothermic reaction chambers 262 may be varied as desired. That is, the catalyst loading may be graded throughout the reforming sections.
  • the combination reaction vessel 54 may include flow directing headers 190 to directing the flow of exhaust exiting the first set of exothermic reaction chambers 264 so that it enters a second set of exothermic reaction chambers that are spaced a distance from the first set.
  • the combustion reaction exhaust exits the vessel through line 245 in the reformation reaction exhaust exits the vessel through line 256 .

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Sustainable Energy (AREA)
  • Sustainable Development (AREA)
  • Manufacturing & Machinery (AREA)
  • Electrochemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • General Health & Medical Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Fuel Cell (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Feeding And Controlling Fuel (AREA)
  • Incineration Of Waste (AREA)

Abstract

A reaction vessel that integrates and balances an endothermic process with at least one exothermic process of the fuel cell system. Preferably the exothermic process is conducted in stages to provide more uniform and/or controllable heat generation and exchange, and to produce a uniform and/or controllable temperature profile in the endothermic reaction process. The invention allows for the elimination of the working fluid loop of prior art systems that had unsatisfactory response times at startup, and during transient conditions, and also added to the overall mass and volume of the fuel cell system.

Description

TECHNICAL FIELD
This invention relates to fuel cell systems and components, and more particularly to a fuel cell system that combines exothermic and endothermic processes in one reaction vessel.
BACKGROUND OF THE INVENTION
Alexander Grove invented the first fuel cell in 1839. Since then most of the fuel cell development has been primarily limited to applications supported by the government, such as the United States National Aeronautics and Space Administration (NASA), or to utility plants applications. However, recent developments in materials of construction and processing techniques have brought fuel cell development closer to significant commercial applications. A primary advantage of fuel cells is that fuel cells can convert stored energy to electricity with about 60–70 percent efficiency, with higher efficiencies theoretically possible. Further, fuel cells produce virtually no pollution. These advantages make fuel cells particularly suitable for vehicle propulsion applications and to replace the internal combustion engine which operates at less than 30 percent efficiency and can produce undesirable emissions.
Although fuel cells are desirable for vehicle propulsion applications, the fuel cell must be incorporated into a complicated on-board system that includes a fuel cell stack and auxiliary equipment. The following brief discussion of the operation and purpose of the fuel cell stack and its auxiliary equipment will be helpful in understanding the advantages and desirability of the present invention.
Fuel Cell Operation
A fuel cell principally operates by oxidizing an element, compound or molecule (that is, chemically combining with oxygen) to release electrical and thermal energy. Thus, fuel cells operate by the simple chemical reaction between two materials such as a fuel and an oxidant. Today, there are a variety of fuel cell operating designs that use many different fuel and oxidant combinations. However, the most common fuel/oxidant combination is hydrogen and oxygen.
In a typical fuel cell, hydrogen is consumed by reacting the hydrogen with oxygen from air to produce water, electrical energy and heat. This is accomplished by feeding the hydrogen over a first electrode (anode), and feeding the oxygen over a second electrode (cathode). The two electrodes are separated by an electrolyte which is a material that allows charged molecules or “ions” to move through the electrolyte. There are several different types of electrolytes that can be utilized including the acid-type, alkaline-type, molten-carbonate-type and solid-oxide-type. The so-called PEM (proton exchange membrane) electrolytes (also known as a solid polymer electrolyte) are of the acid-type, and potentially have high-power and low-voltage, and thus are desirable for vehicle applications.
FIG. 1 shows a fuel cell that has been simplified for purposes of illustrating the operation of a fuel cell. In the proton exchange membrane based fuel cell 10 shown, a hydrogen gas stream 12 is fed into a first sealed chamber or manifold (in the case of a fuel cell stack) 14 and over a first electrode (anode) 24 and on to a first face 16 (the anode side) of a proton exchange membrane assembly assembly 18. The proton exchange membrane assembly 18 typically includes the electrolyte membrane 19 having two faces, and on each face there is a catalyst, usually a noble metal such as platinum, and an electrically conductive diffusion media (such as a carbon fiber mat) overlying the catalyst. The catalyst and diffusion media are not shown in FIG. 1. The catalyst on the anode face of the assembly promotes the dissociation of hydrogen molecules and the catalyst on the cathode face of the assembly promotes the dissociation of oxygen molecules and a reaction of oxygen with hydrogen protons to produce water. The electrolyte membrane 19 allows the diffusion of hydrogen ions 26 from one electrode 24 to another electrode 34. FIG. 1 is a simple illustration attempting to depict the diffusion of these hydrogen ions 26 from the anode to the cathode side of the electrolyte membrane. However, the electrolyte membrane 19 does not include channels as shown in FIG. 1.
A compressed air stream 22 is supplied to a second chamber or manifold (for a fuel cell stack) 15 in a manner so that the compressed air flows over a second electrode (cathode) 34 and on to a second face 20 of the proton exchange membrane assembly 18. The proton exchange membrane assembly 18 is selective and allows only the hydrogen protons 26 to pass through the membrane assembly 18 rejecting larger diatomic hydrogen molecules 28. When a single hydrogen proton (or its equivalent) 26 passes through the membrane, it leaves behind an electron 30. The electrons 30 that are left behind can be collected in the electrode (conductor) 24. Typically fuel cell systems include a stack of single cells (fuel cell stack) with adjacent cells sharing a common electrode. In that case, the electrodes 24, 34 would be bipolar. Preferably each electrode 24, 34 includes channels 25 formed therein through which either hydrogen or oxygen flows.
The concentrated electrons in the electrode 24 causes a potential negative voltage on the electrode 24 due to the excess of electrons (because the electrons are negatively charged). When the oxygen molecules are directed to the second face 20 of the proton exchange membrane assembly 18, the oxygen meets the hydrogen proton 26 as the proton passes through the membrane. The chemical reaction of the hydrogen proton 26 and the oxygen on the cathode side of the cell requires electrons and therefore a shortage of electrons is created. The needed electrons can be supplied by a second electrode 34 (that is, the cathode electrode). The oxygen and the hydrogen proton 26, in the presence of the electrons 30 from the second electrode 34, easily combined to produce water 32. The reactions at the electrodes are as follows:
Anode 2H2→4H++4e−
Cathode O2+4e−+4H+→2H2O.
With two electrodes 24, 34 in the fuel cell system (the anode and the cathode) an electrical potential exist between the two electrodes. That is, the hydrogen electrode 24 has an excess of electrons and the oxygen electrode 34 needs electrons. The electrical potential can be utilized by placing an electrical load, such as electrical motor 36 (to propel a vehicle) between the anode 24 and the cathode 34. Since electrical energy is used as it goes around the loop, the only by-products of this fuel system are water vapor and the heat loss through inefficiency of the cell itself (or about 30 percent of the power). With 70 percent efficiency, this process is significantly more attractive for extracting stored energy than an internal combustion engine that typically extracts only 20–30 percent of stored fuel energy.
Both hydrogen and oxygen are each supplied to the fuel cell in excess to provide the greatest rate of reaction possible. The hydrogen gas stream will be under pressure of about 3 bars if it is produced from a fuel reformation reaction and therefore the oxygen stream 22 must be pumped up to the same pressure to avoid damage to the proton exchange membrane and the catalyst of the assembly 18. Any water produced or remaining on either side of the fuel cell is removed and is discharged or may be sent through a water/vapor stream line 38 to a water reservoir (such as the holding tank 46 shown in FIG. 2) for use in other components or for use in the fuel cell at startup. The effluent or tail gas exhaust stream 40, 42 from both sides of the fuel cell are discharged to the atmosphere or preferably are supplied to a combustor for burning and producing heat needed for other operations such as the fuel reformation process described hereafter. Since the reactants are supplied to the fuel cell in excess, tail gas exhaust stream 40 from the anode side contains hydrogen and the tail gas exhaust stream 42 from the cathode side contains oxygen. Both of the fuel cell tail gas streams 40, 42 may be combusted in a catalytic combustor to provide heat for other components in the fuel cell system.
Preferably the fuel cell is maintained at a temperature of about 80 degrees Celsius or greater. Maintaining this temperature may require heat to be added or removed from the fuel cell stack. Often heat must be supplied to the fuel cell at startup. This heat can be supplied by a catalytic or flame combustor. However, during post startup or normal operation of the fuel cell, heat is generated by the fuel cell and the generated heat can be removed by any of a variety of heat exchange methods but preferably is removed using a liquid coolant.
Auxiliary Equipment
As will be appreciated from the forgoing, fuel cell systems require a variety of auxiliary equipment such as pumps, heat exchangers, fuel processors, combustors, water separation and collection equipment, hydrogen cleanup or purification systems and so on to support the operation of the fuel cell itself. Auxiliary equipment that is of interest with respect to this invention is discussed below.
Although compressed or liquefied hydrogen could be used to operate a fuel cell in a vehicle, to date this is not practical. The use of compressed or liquefied hydrogen ignores the extensive infrastructure currently being used to supplying gasoline for internal combustion engine automobiles and trucks. Consequently, it is more desirable to utilize a fuel such as methanol, gasoline, diesel, methane and the like to provide a hydrogen source for the fuel cell. However, the methanol, gasoline, diesel, methane and the like must be reformed to provide a hydrogen gas source. This is accomplished by using methanol or gasoline fuel processing or reforming equipment, and hydrogen cleanup or purification equipment.
Fuel cell systems often include a fuel processing section which reforms the fuel such as methanol, gasoline, diesel, methane and the like to produce hydrogen and a variety of other byproducts. However, these reforming (reformation) processes are endothermic and require energy input to drive the reformation reaction.
Typically, a catalytic or flame combustor is utilized to provide heat for the reforming process. Most often, this is accomplished by utilizing a working fluid (liquid or gas) loop that transfers heat from the combustion process to the reforming process. However, the response time for heat transfer needed during startup and transient conditions of the fuel cell are less than optimal when the system uses a fluid to transfer heat between the combustor and the reformer vessel. Further, the working fluid loop, associated heat exchangers and piping add to the overall mass and volume of the fuel cell system.
Thus it would be desirable to provide a low-cost, low-weight system for supplying heat to a fuel cell reforming process and wherein the system is responsive to the heat load fluctuations of the reforming process. The present invention overcomes some of the inefficiencies of the prior art
SUMMARY OF INVENTION
The invention includes a reaction vessel that integrates and balances an endothermic process with at least one exothermic process of a fuel cell system. Preferably the exothermic process is conducted in stages to provide more uniform and/or controllable heat generation and exchange, and to produce a uniform, and/or controllable temperature profile in the endothermic reaction process, if desired (depending on the fuel used). The invention eliminates the working fluid heat exchange loop of prior art fuel reforming sections that had unsatisfactory response times at startup, and during transient conditions, and also added to the overall mass and volume of the fuel cell system.
One embodiment of the invention includes a reaction vessel having an outer shell and catalyst carried in the shell for promoting an endothermic reaction. The reaction vessel is constructed and arranged to charge an endothermic reactant(s) into the shell. A plurality of heat exchanger devices are also provided having portions separately positioned and carried within the shell. Each heat exchanger device is independently controlled from the other heat exchanger devices so that heat transferred by the heat exchanger devices to the catalyst, and the temperature of the catalyst in the shell, may be varied at different locations within the reaction vessel. Preferably the reaction vessel is constructed and arranged so that exothermic reactants may be charged into each heat exchanger device and combusted to generate heat for driving the endothermic reaction occurring in another portion of the reaction vessel. The exothermic reactants may include anode and cathode exhaust streams from a fuel cell stack.
Another embodiment of the present invention includes a reaction vessel having a plurality of endothermic reaction sections and a plurality of heat transfer devices. Each heat transfer device is associated with an endothermic reaction section so that sufficient heat may be transferred to the endothermic reaction section and so as to control the temperature profile of the endothermic reaction section within a predetermined range. The endothermic reaction sections may be spaced apart from each other and so that a heat transfer device is positioned between adjacent spaced apart endothermic reaction sections.
Another embodiment of the present invention includes a combination reaction vessel having multiple staged catalytic combustion chambers and a plurality of endothermic reaction chambers. Each endothermic reaction chamber has a combustion chamber adjacent thereto so that heat generated in the combustion chamber is transferred to the adjacent endothermic reaction chamber. Each catalytic combustion chamber may have a plurality of reactant charge openings for supplying at least one reactant to the catalytic combustion chamber. The charge openings may be positioned within the catalytic combustion chamber to provide a substantially uniform temperature along the length of the catalytic combustion chamber.
Another embodiment of the invention includes a charge manifold having a plurality of charge pipes extending therefrom. Each charge pipe extends into an exothermic reaction chamber. The charge pipes have charge holes provided along the length of each charge pipe so the fuel or oxidant may be charged into the combustion reaction chamber through the charge holes. Preferably valves are associated with each charge pipe and a controller is provided for selectively controlling the amount of fuel or oxidant charged to each exothermic reaction chamber. Each charge pipe may separate adjacent side-by-side exothermic reaction chambers. A directional flow header may be provided at the end of each exothermic reaction chamber for directing gases exiting one exothermic reaction chamber to the entrance of an adjacent side-by-side exothermic reaction chamber.
Another embodiment of present invention includes the incorporation of a fuel/water vaporizer into the combination reaction vessel. A fuel/water mixture is injected into a plurality of vaporization chambers and is vaporized by heat generated by the catalytic combustion of a fuel mixture charged into a plurality of exothermic reaction chambers. No catalyst is provided in the vaporization chambers. An oxidant and fuel are charged into the exothermic reaction chambers and catalytically combusted to produce heat to vaporize the fuel/water mixture.
Another embodiment of present invention includes a combination reaction vessel that incorporates an exothermic and endothermic reaction. The reaction vessel includes a plurality of endothermic reaction chamber sections that are spaced apart vertically and horizontally. A plurality of exothermic reaction chamber sections are also provided in a spaced apart fashion so that a partition section is provided between laterally spaced apart exothermic reaction chamber sections. The partition sections provide for staged adiabatic reforming of the fuel/water mixture. The catalyst loading in different portions of the endothermic reaction chamber sections may be varied as desired.
These and other objects, features and advantages of present invention will become apparent from the following brief description of drawings, detailed description of preferred embodiments, and appended claims and drawings.
BRIEF DESCRIPTION OF THE DRAWINGS
FIG. 1 illustrates a fuel cell useful in the present invention;
FIG. 2 is a schematic illustration of a fuel cell system useful in a present invention;
FIG. 3 is a sectional view of a combination reaction vessel for housing an endothermic and an exothermic reaction according to the present invention;
FIG. 4 is a sectional view of an alternative embodiment of a combination reaction vessel for housing an endothermic and an exothermic reaction according to the present invention;
FIG. 5 is a sectional view of an alternative embodiment of a combination reaction vessel for housing an endothermic and an exothermic reaction according to the present invention;
FIG. 6 is an exploded, prospective view, with portions broken away, of an alternative embodiment of a combination reaction vessel for housing an endothermic and an exothermic reaction according to the present invention; and
FIG. 7 is a sectional view of an alternative embodiment of a reaction vessel for housing a staged endothermic reaction according to the present invention.
 DESCRIPTION OF THE PREFERRED EMBODIMENT
Referring now to FIG. 2, the fuel cell system according to the present invention includes a fuel cell (or fuel cell stack) 10. The system may also include the following auxiliary equipment to support the fuel cell stack 10. Water is provided and held in a water reservoir or holding tank 46 which is connected to a vaporizer 48 by water line 44. A fuel source is provided and held in a tank 52 that is also connected to the vaporizer 48 by line 50. Preferably the fuel used is methanol, gasoline, diesel, methane and the like. The fuel and water may be vaporized by any method known to those skilled in the art, but preferably the heat for the vaporization step is supplied by a heat exchanger 39 in the vaporizer that catalytically combusts hydrogen 40′ and oxygen 42′ from the fuel cell stack 10 exhaust. Alternatively, the vaporizer may be included as an integral part of the reaction vessel 54 as will be described hereafter. The fuel and water are vaporized together (or may be vaporized separately) and a resultant vaporized fuel/water stream is delivered via line 58 to an endothermic reaction section of a combination reaction vessel 54. Preferably a fuel reformation process is conducted in the endothermic reaction section.
The combination reaction vessel 54 also houses an exothermic reaction section. The exothermic reaction may be, for example, catalytic combustion of a fuel or preferential oxidation of the exhaust stream from the fuel reforming section. If the exothermic reaction process is catalytic combustion, preferably the anode exhaust stream 40 and cathode exhaust stream 42 from the fuel cell 10 are used as the catalytic combustion reactants. The exhaust from the exothermic reaction may be discharged to the atmosphere via line 43.
The reformation process effluent stream 56 may include hydrogen molecules (H2), CO, CO2, N2, CH4. The reformation process effluent stream 56 may be delivered to a hydrogen purification section 59 to reduce the concentration of CO and hydrocarbons (or carbon based molecules). The hydrogen purification section 59 may include any of a variety of components for purifying the reformation process effluent stream 56 and may include high and low temperature reactors to shift the equilibrium of the stream 56 constituents (thus reducing the concentration of CO), preferential oxidation reactor(s), additional hydrocarbon reforming components, separators, adsorbers and similar equipment. Eventually a hydrogen rich stream 60 is delivered to the anode side of the fuel cell 10.
As indicated earlier, air 22 is pumped to the cathode side of the fuel cell 10. The anode and cathode exhaust streams from the fuel cell stack carry water that can be condensed out using a separator/condenser as the stream exits fuel cell stack and the liquid water may be sent to reservoir 46. Alternatively, the water may be condensed out after the stack effluent passes through exhaust tail gas combustors.
FIG. 3 illustrates a combination reaction vessel 54 for housing an endothermic and an exothermic reaction. The combination reaction vessel 54 includes an endothermic reaction chamber section 62 and an exothermic reaction chamber section 64 that share a common wall or substrate 66. Each endothermic reaction chamber section 62 and exothermic reaction chamber section 64 includes an associated outside wall 68, 70 respectively. A catalyst 61 for promoting the reformation reaction of the fuel and water, is provided in the endothermic reaction chamber section 62. As illustrated in FIG. 3 the catalyst 61 may overlie at least one of the outside wall 68 and/or the substrate 66. The catalyst 61 may be provided directly on the outside wall 68 or the substrate 66, or intermediate layers (not shown) may be provided therebetween. The vaporized fuel and water mixture may enter the endothermic reaction chamber section 62 from one end 72 or may be selectively charged to the endothermic reaction chamber through charge lines 74 or openings 75 selectively positioned along the length of the endothermic reaction chamber section 62. The term “endothermic reactants” as used herein means reactants of an endothermic reaction. In this case, for example, the endothermic reactants are the organic fuel and water.
The exothermic reaction chamber section 64 may be similarly constructed. As illustrated in FIG. 3, an exothermic catalyst 65 may overlie at least one of the outside wall 70 or substrate 66. Similarly, the catalyst 65 may be provided directly on the outside wall 70 or the substrate 66, or intermediate layers (not shown) may be provided therebetween. In one embodiment of the invention, a fuel combustion process may be conducted in the exothermic reaction chamber 64. An oxidant such as oxygen (from air) may be charged into the chamber section 64 through one end 76 of the chamber and a fuel such as hydrogen or a hydrocarbon may be supplied to the chamber through one or more charge lines 74′ or through a charge openings 75′ that may be positioned along the length of the exothermic reaction chamber section 64. Alternatively, the fuel may be charged through the open end 76 and the oxidant supplied through the charge lines 74′ or charge openings 75′. In another embodiment, an exothermic reaction such as a preferential oxidation reaction to reduce CO or hydrocarbons may be conducted in the exothermic reaction chamber section 64. In any event, the heat generated by the exothermic reaction in the exothermic reaction chamber section 64 is transferred through the substrate 66 to warm the endothermic reaction chamber section 62, catalyst 61 and reactants, and to drive (that is, to provide the heat necessary to complete the reaction) the endothermic reaction process. The term “exothermic reactants” as used herein means the reactants of an exothermic reaction. The exothermic reactants may include a fuel such as an organic fuel including, for example, hydrogen, methanol, gasoline, diesel, methane and the like; and an oxidant, such as oxygen in the form of air.
FIG. 4 illustrates an alternative embodiment of the present invention wherein either the endothermic or the exothermic catalyst may be provided on a solid porous substrate 78 or porous pellets 80 or any of a variety materials that would provide increased surface area for either of the catalysts. When the catalyst is on a high surface area material such as a porous block or porous pellets that are carried in the chamber, the catalyst is also considered to be overlying the substrate for purposes of this invention.
FIG. 5 illustrates an alternative embodiment of the present invention wherein a reactant charge pipe 82 extends into one of the reaction chambers 62, 64 and has a plurality of discharge holes 84 formed therein along the length of the reaction chamber to selectively discharge a reactant into the chamber at predetermined locations. Preferably, the charge pipe 82 delivers a fuel such as hydrogen to the combustion reaction chamber 64 which has an oxidant such as oxygen or air flowing therein. Alternatively, the charge pipe 82 may be used to introduce oxygen to allow for staged preferential oxidation. The use of the reactant charge pipe 82 with discharge holes 84 allows the fuel or oxidant to be supplied in relatively low concentrations so as to reduce the risk of autoignition and also to provide a more uniform heat generation profile along the length of the exothermic reaction chamber 64. Of course, porous catalyst pellets or another suitable supported catalyst may be provided in the exothermic reaction chamber 64.
The substrate 66 (shown in FIGS. 3–5) may be made from a variety of materials having suitable heat transfer characteristics and may include any of several metals such as stainless-steel, copper, aluminum, or any of a variety of composites, ceramics, compounds or polymer base materials.
As described earlier, when the exothermic reaction produces heat, the heat is transferred through the substrate wall 66 separating an adjacent set of chambers 62, 64. As such, the combination reaction vessel provides a staged exothermic reaction process (preferably combustion of a fuel) to provide a uniform temperature profile and heat transfer to drive an endothermic reaction (preferably a fuel reforming process) occurring in an adjacent chamber.
Referring now to FIG. 6, another embodiment of the present invention includes a combination reaction vessel 54 having a plurality of spaced apart, parallel endothermic reaction chambers 62. In this case the endothermic reaction chambers 62 are vertically spaced apart and separated by an exothermic reaction chamber 64 that has a longitudinal axis and flow path running in a perpendicular direction to the longitudinal axis and flow path of the endothermic reaction chamber 62. However, parallel co-flowing and counter flow configurations are contemplated as a part of the present invention. As described earlier, an endothermic reaction catalyst is provided in each of the endothermic reaction chambers 62 and the endothermic reactants, such as a methanol/water, gasoline/water vapor mixture, or other fuel/water mixture are supplied through one end 72 (see also FIG. 3) of the endothermic reaction chamber and flow in the direction indicated by arrow shown entering the reaction chamber 62 in FIG. 6.
A plurality of spaced apart parallel exothermic reaction chambers 64 are provided so that each exothermic chamber 64 separates two endothermic reaction chambers 62 so as to provide a staged exothermic reaction process. The exothermic chambers 64 may also be arranged in a laterally adjacent side-by-side configuration. An inlet header 86 is provided having an inlet opening 88 formed therein through which at least one of the exothermic reactants is charged to the exothermic reaction chambers 64. Preferably, exhaust gas (which contains oxygen) from the cathode side of the fuel cell is feed through the inlet opening 88. The cathode exhaust gas flows down a first set of exothermic reaction chambers and is directed by a flow directing header 90 down a second set of exothermic reaction chambers, and so on in a serpentine fashion throughout the combination reaction vessel 54 and finally exits through an exhaust opening 92 formed in an outlet header 94.
A second exothermic reaction reactant may be charged into the exothermic reaction chambers 64 utilizing a charge manifold 96. In a preferred embodiment, the charge manifold 96 includes a plurality of charge pipes or lines 82. A charge pipe 82 is received in one of each of the exothermic reaction chambers 64. Preferably, the charge pipe 82 has a plurality of discharge holes 84 which are spaced apart along the length of the exothermic reaction chamber (as also shown in FIG. 5). The combination reaction vessel 54 may be constructed and arranged so that the charge pipes 82 also function to separate laterally adjacent side-by-side exothermic reaction chambers. That is, the charge crepe 82 acts as a wall separating laterally adjacent exothermic reaction chambers. Because the exothermic reaction chambers 64 are staged in sections and at least one reactant is selectively and/or uniformly charged to each chamber along the length of the exothermic chamber, the heat generated throughout the exothermic reaction chamber may be controlled so that it is substantially uniform, or graduated is so desired. Consequently, the heat transferred to the endothermic reaction chamber, catalyst and reactants is such that the temperature profile in the endothermic reaction chamber is controlled to be substantially uniform, or graduated if so desired. Maintaining a controllable temperature profile in a fuel reforming process is important to avoid undesirable side effects such as catalyst degradation, or methane slip. At low power, the temperature profile may be such as to promote a high temperature reformation with a high temperature shift reaction at the exit of the reaction chamber. The temperature at the exit end of the reaction chamber should be high enough to suppress methane formation for a given catalyst.
A plurality of temperature or concentrations sensors 104 may be selectively placed in the combination reaction vessel, and valves 100 may be included in the charge manifold 96 to selectively control the amount of reactant being charged to the chamber and thus control the reaction as desired. Associated on-board computer controllers 102, drivers and associated electrical equipment can be provided to control the above described components and processes in a manner known to those skilled in the art.
For example, in a methanol reformer, the charge manifold 96 may be constructed and arranged to controllably charge reactants so that a uniform temperature profile at full power is provided which would utilize the entire reactor volume. However, under turndown situations (for example, when the vehicle is stopped), less power is require, and thus only a portion of the reactor is required to reform fuel because of the lower power demand. In these turndown situations it may be desirable to control the exothermic reaction adjacent to each endothermic reaction chamber section so that only selected endothermic reaction chamber sections or portions of selected endothermic reaction chambers sections are provided with enough heat to reform fuel. The remaining endothermic reaction sections or portions thereof could be utilized to perform a water gas shift reaction to reduce the concentration of CO in the fuel reforming stream. For example, the temperature in the first two endothermic reaction sections could be controlled to provide relatively high temperature fuel reforming and the temperature in the remaining endothermic reaction sections (that is, in the rearward portion of the reaction vessel) could be controlled to be relatively low thereby reducing unwanted reformation byproducts and so that a maximum conversion is accomplished during the fuel reforming while minimizing methane slip.
An another embodiment, illustrated in FIG. 7, the vaporizer may be included in the front portion of the combination reaction vessel 54. The combination reaction vessel shown in FIG. 7 operates similarly to the vessel shown in FIG. 2, but with a few exceptions. In this embodiment, a fuel/water mixture may be charge through line 258 into a first section of the combination reaction vessel 54 to be vaporized in a first heat exchanger section 202. The fuel/water mixture flows through a plurality of spaced apart chamber 262′ that do not include a fuel reforming catalyst. Thereafter, the endothermic reaction chambers 262 include a fuel reforming catalyst as previously discussed.
The fuel/water mixture entering the chambers 262′ is vaporized by heat generated by the catalytic combustion of a combustion fuel mixture charged into a plurality of exothermic reaction chambers 264. An oxidant or fuel, preferably an oxidant such as oxygen from the fuel cell stack effluent, may be charged to the exothermic reaction chambers 264 through a charge line 242 and header 243. An oxidant or fuel, preferably a fuel such as hydrogen from the fuel cell stack effluent, is charged to the exothermic reaction chambers 264 through charge line 282. A combustion fuel mixture travels through the plurality of spaced apart exothermic reaction chambers 264 generating heat to vaporize the fuel/water mixture or reform the fuel/water mixture. Preferably one of the oxidant or fuel is charged to the exothermic reaction chambers 264 through charge lines 282 in a staged fashion as previously discussed. However, in this embodiment, the exothermic reaction chambers 264 to are spaced apart vertically and horizontally so that a partition section 299 is provided between laterally spaced apart exothermic reaction chambers 264. The partition sections 299 provide for staged adiabatic reformation of the fuel/water mixture. If desired, the catalyst loading in different portions of the endothermic reaction chambers 262 may be varied as desired. That is, the catalyst loading may be graded throughout the reforming sections. The combination reaction vessel 54 may include flow directing headers 190 to directing the flow of exhaust exiting the first set of exothermic reaction chambers 264 so that it enters a second set of exothermic reaction chambers that are spaced a distance from the first set. The combustion reaction exhaust exits the vessel through line 245 in the reformation reaction exhaust exits the vessel through line 256.

Claims (6)

1. A fuel cell system comprising:
a reaction vessel having a catalyst carried in the vessel for promoting an endothermic reaction, the reaction vessel being constructed and arranged to allow endothermic reactants to be charged into the vessel, and further comprising at least a first and a second heat exchanger device spaced apart from each other and carried within the vessel, and wherein the first and second heat exchanger devices are constructed and arranged to be independently controlled from each so that heat transferred by the heat exchanger devices to the catalyst, and the temperature of the catalyst, may be varied at different locations within the reaction vessel corresponding to the location of the first and second heat exchanger devices, and wherein the reaction vessel comprises a plurality of parallel substrates, each of the substrates having a first and a second surface, and wherein the first and second surfaces are located on opposite sides of the substrate, and an endothermic reaction catalyst overlying the first surface, and an exothermic reaction catalyst overlying the second surface, and wherein each of the substrates is constructed and arranged to transfer heat from the second surface to the first surface.
2. A fuel cell system as set forth in claim 1 wherein the reaction vessel is constructed and arranged so that exothermic reactants may be charged into each heat exchanger device and wherein the exothermic reactants comprising a fuel and an oxidant, and wherein each of the heat exchanger devices includes at least one combustion chamber, and wherein at least one of the fuel and the oxidant are selectively charged to each combustion chamber in a controlled amount so that the heat generated by each of the heat exchanger devices may be varied as desired.
3. A fuel cell system comprising:
a reaction vessel integrating an exothermic reaction and an endothermic reaction, the reaction vessel including a plurality of substrates, each of the substrates having a first and a second surface, and wherein the first and second surfaces are located on opposite sides of the substrate, and an endothermic reaction catalyst overlying the first surface, and an exothermic reaction catalyst overlying the second surface, and wherein each of the substrates is constructed and arranged to transfer heat from the second surface to the first surface.
4. A fuel cell system as set forth in claim 3 wherein the substrate comprises at least one of stainless steel, copper, aluminum, a composite or polymer based materials.
5. A fuel cell system as set forth in claim 3 wherein the substrate has a substantially flat planar configuration.
6. A fuel cell system as set forth in claim 1 wherein the substrate comprises a metal comprises comprising at least one of stainless steel, copper or aluminum.
US09/669,969 2000-09-26 2000-09-26 Multiple stage combustion process to maintain a controllable reformation temperature profile Expired - Lifetime US7081312B1 (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
US09/669,969 US7081312B1 (en) 2000-09-26 2000-09-26 Multiple stage combustion process to maintain a controllable reformation temperature profile
DE10147368A DE10147368A1 (en) 2000-09-26 2001-09-25 Fuel cell system for vehicle, has reaction vessel with catalyser carried that delivers endothermic reaction and arranged so that endothermic reactants can be supplied to vessel.
JP2001294237A JP2002198074A (en) 2000-09-26 2001-09-26 Multi-stage combustion process to maintain a controllable reforming temperature profile
US10/962,651 US7993784B2 (en) 2000-09-26 2004-10-12 Multiple stage combustion process to maintain a controllable reformation temperature profile
US10/962,802 US7842424B2 (en) 2000-09-26 2004-10-12 Multiple stage combustion process to maintain a controllable reformation temperature profile

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US09/669,969 US7081312B1 (en) 2000-09-26 2000-09-26 Multiple stage combustion process to maintain a controllable reformation temperature profile

Related Child Applications (2)

Application Number Title Priority Date Filing Date
US10/962,802 Division US7842424B2 (en) 2000-09-26 2004-10-12 Multiple stage combustion process to maintain a controllable reformation temperature profile
US10/962,651 Division US7993784B2 (en) 2000-09-26 2004-10-12 Multiple stage combustion process to maintain a controllable reformation temperature profile

Publications (1)

Publication Number Publication Date
US7081312B1 true US7081312B1 (en) 2006-07-25

Family

ID=24688469

Family Applications (3)

Application Number Title Priority Date Filing Date
US09/669,969 Expired - Lifetime US7081312B1 (en) 2000-09-26 2000-09-26 Multiple stage combustion process to maintain a controllable reformation temperature profile
US10/962,802 Expired - Fee Related US7842424B2 (en) 2000-09-26 2004-10-12 Multiple stage combustion process to maintain a controllable reformation temperature profile
US10/962,651 Expired - Fee Related US7993784B2 (en) 2000-09-26 2004-10-12 Multiple stage combustion process to maintain a controllable reformation temperature profile

Family Applications After (2)

Application Number Title Priority Date Filing Date
US10/962,802 Expired - Fee Related US7842424B2 (en) 2000-09-26 2004-10-12 Multiple stage combustion process to maintain a controllable reformation temperature profile
US10/962,651 Expired - Fee Related US7993784B2 (en) 2000-09-26 2004-10-12 Multiple stage combustion process to maintain a controllable reformation temperature profile

Country Status (3)

Country Link
US (3) US7081312B1 (en)
JP (1) JP2002198074A (en)
DE (1) DE10147368A1 (en)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050048332A1 (en) * 2000-09-26 2005-03-03 General Motors Corporation Multiple stage combustion process to maintain a controllable reformation temperature profile
US20080292922A1 (en) * 2007-05-22 2008-11-27 Fischer Bernhard A Method and apparatus for fueling a solid oxide fuel cell stack assembly
US20090311566A1 (en) * 2008-06-12 2009-12-17 Hyundai Motor Company Separating plate for fuel cell stack and method of manufacturing the same
US20120020851A1 (en) * 2002-01-04 2012-01-26 Meggitt (Uk) Limited Reformer Apparatus and Method

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7220390B2 (en) * 2003-05-16 2007-05-22 Velocys, Inc. Microchannel with internal fin support for catalyst or sorption medium
US7306868B2 (en) * 2003-10-02 2007-12-11 Hewlett-Packard Development Company, L.P. Integrated fuel cell stack and catalytic combustor apparatus, assembly, and method of use
US7470408B2 (en) * 2003-12-18 2008-12-30 Velocys In situ mixing in microchannels
GB0408896D0 (en) * 2004-04-20 2004-05-26 Accentus Plc Catalytic reactor
JP2006265007A (en) * 2005-03-22 2006-10-05 Toyota Motor Corp Fuel reformer
JP4405432B2 (en) * 2005-05-23 2010-01-27 本田技研工業株式会社 Reformer
JP2007091565A (en) * 2005-09-30 2007-04-12 Nissan Motor Co Ltd Fuel modification reactor
US20070122667A1 (en) * 2005-11-28 2007-05-31 Kelley Richard H Fuel cell system with integrated fuel processor
JP5214230B2 (en) * 2007-12-04 2013-06-19 Ｊｘ日鉱日石エネルギー株式会社 Starting method of fuel cell system
US7745667B2 (en) * 2008-04-07 2010-06-29 Velocys Microchannel apparatus comprising structured walls, chemical processes, methods of making formaldehyde
US20100143755A1 (en) * 2009-06-24 2010-06-10 Fischer Bernhard A Multi-Channel Fuel Reformer with Augmented Heat Transfer
KR101035663B1 (en) * 2009-07-21 2011-05-19 한국에너지기술연구원 Medium circulation combustor and medium circulation combustion method using the same
WO2016124567A1 (en) * 2015-02-05 2016-08-11 Casale Sa Burner for the production of synthesis gas and related cooling circuit
CN114824386B (en) * 2022-03-25 2024-02-23 清华大学 Fuel pretreatment device and fuel cell system

Citations (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4650727A (en) 1986-01-28 1987-03-17 The United States Of America As Represented By The United States Department Of Energy Fuel processor for fuel cell power system
US4781241A (en) 1987-08-27 1988-11-01 International Fuel Cells Corporation Heat exchanger for fuel cell power plant reformer
US5043232A (en) 1990-05-10 1991-08-27 International Fuel Cells Corporation Fuel Preheating for a fuel processing system of a fuel cell power plant
US5175062A (en) 1991-01-30 1992-12-29 Energy Research Corporation Reforming unit for fuel cell stack
US5272017A (en) 1992-04-03 1993-12-21 General Motors Corporation Membrane-electrode assemblies for electrochemical cells
US5470670A (en) 1993-03-01 1995-11-28 Matsushita Electric Industrial Co., Ltd. Fuel cell
US5670269A (en) 1994-07-05 1997-09-23 Ishikawajima-Harima Heavy Industries, Co., Ltd. Molten carbonate power generation system with plate reformer
US5763114A (en) * 1994-09-01 1998-06-09 Gas Research Institute Integrated reformer/CPN SOFC stack module design
US5780179A (en) 1995-06-26 1998-07-14 Honda Giken Kogyo Kabushiki Kaisha Fuel cell system for use on mobile bodies
US5851689A (en) 1997-01-23 1998-12-22 Bechtel Corporation Method for operating a fuel cell assembly
US5997594A (en) * 1996-10-30 1999-12-07 Northwest Power Systems, Llc Steam reformer with internal hydrogen purification
US6183703B1 (en) * 1996-04-12 2001-02-06 Ztek Corporation Thermally enhanced compact reformer
US20020071797A1 (en) * 2000-10-06 2002-06-13 Loffler Daniel G. Catalytic separator plate reactor and method of catalytic reforming of fuel to hydrogen
US6472092B1 (en) * 1998-08-12 2002-10-29 Honda Giken Kogyo Kabushiki Kaisha Fuel-reforming apparatus comprising a plate-shaped reforming catalyst
US6797244B1 (en) * 1999-05-27 2004-09-28 Dtc Fuel Cells Llc Compact light weight autothermal reformer assembly

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US962802A (en) * 1908-04-20 1910-06-28 Sakichi Toyoda Picker-check for looms.
US962651A (en) * 1910-03-24 1910-06-28 F K De Borde Sea power-generator.
US4877693A (en) * 1985-12-23 1989-10-31 Energy Research Corporation Fuel cell apparatus for internal reforming
CN1094465C (en) * 1996-06-28 2002-11-20 松下电工株式会社 Modification apparatus
US7066973B1 (en) * 1996-08-26 2006-06-27 Nuvera Fuel Cells Integrated reformer and shift reactor
JP2000034102A (en) * 1998-07-17 2000-02-02 Toyota Motor Corp Reformer control device
US6238815B1 (en) * 1998-07-29 2001-05-29 General Motors Corporation Thermally integrated staged methanol reformer and method
US6969506B2 (en) * 1999-08-17 2005-11-29 Battelle Memorial Institute Methods of conducting simultaneous exothermic and endothermic reactions
US7081312B1 (en) 2000-09-26 2006-07-25 General Motors Corporation Multiple stage combustion process to maintain a controllable reformation temperature profile

Patent Citations (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4650727A (en) 1986-01-28 1987-03-17 The United States Of America As Represented By The United States Department Of Energy Fuel processor for fuel cell power system
US4781241A (en) 1987-08-27 1988-11-01 International Fuel Cells Corporation Heat exchanger for fuel cell power plant reformer
US5043232A (en) 1990-05-10 1991-08-27 International Fuel Cells Corporation Fuel Preheating for a fuel processing system of a fuel cell power plant
US5175062A (en) 1991-01-30 1992-12-29 Energy Research Corporation Reforming unit for fuel cell stack
US5272017A (en) 1992-04-03 1993-12-21 General Motors Corporation Membrane-electrode assemblies for electrochemical cells
US5316871A (en) 1992-04-03 1994-05-31 General Motors Corporation Method of making membrane-electrode assemblies for electrochemical cells and assemblies made thereby
US5470670A (en) 1993-03-01 1995-11-28 Matsushita Electric Industrial Co., Ltd. Fuel cell
US5670269A (en) 1994-07-05 1997-09-23 Ishikawajima-Harima Heavy Industries, Co., Ltd. Molten carbonate power generation system with plate reformer
US5763114A (en) * 1994-09-01 1998-06-09 Gas Research Institute Integrated reformer/CPN SOFC stack module design
US5780179A (en) 1995-06-26 1998-07-14 Honda Giken Kogyo Kabushiki Kaisha Fuel cell system for use on mobile bodies
US6183703B1 (en) * 1996-04-12 2001-02-06 Ztek Corporation Thermally enhanced compact reformer
US5997594A (en) * 1996-10-30 1999-12-07 Northwest Power Systems, Llc Steam reformer with internal hydrogen purification
US5851689A (en) 1997-01-23 1998-12-22 Bechtel Corporation Method for operating a fuel cell assembly
US6472092B1 (en) * 1998-08-12 2002-10-29 Honda Giken Kogyo Kabushiki Kaisha Fuel-reforming apparatus comprising a plate-shaped reforming catalyst
US6797244B1 (en) * 1999-05-27 2004-09-28 Dtc Fuel Cells Llc Compact light weight autothermal reformer assembly
US20020071797A1 (en) * 2000-10-06 2002-06-13 Loffler Daniel G. Catalytic separator plate reactor and method of catalytic reforming of fuel to hydrogen

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Fuel Cell Information, "Fuel Cells-a long primer", www.slip.net/~h2man/fuelcell.htm.

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050048332A1 (en) * 2000-09-26 2005-03-03 General Motors Corporation Multiple stage combustion process to maintain a controllable reformation temperature profile
US20050048333A1 (en) * 2000-09-26 2005-03-03 General Motors Corporation Multiple stage combustion process to maintain a controllable reformation temperature profile
US7842424B2 (en) 2000-09-26 2010-11-30 Gm Global Technology Operations, Inc. Multiple stage combustion process to maintain a controllable reformation temperature profile
US7993784B2 (en) 2000-09-26 2011-08-09 GM Global Technology Operations LLC Multiple stage combustion process to maintain a controllable reformation temperature profile
US20120020851A1 (en) * 2002-01-04 2012-01-26 Meggitt (Uk) Limited Reformer Apparatus and Method
US8882865B2 (en) * 2002-01-04 2014-11-11 Meggitt (Uk) Ltd. Reformer apparatus and method with heat exchange occurring through a cross-flow configuration
US20080292922A1 (en) * 2007-05-22 2008-11-27 Fischer Bernhard A Method and apparatus for fueling a solid oxide fuel cell stack assembly
US20090311566A1 (en) * 2008-06-12 2009-12-17 Hyundai Motor Company Separating plate for fuel cell stack and method of manufacturing the same

Also Published As

Publication number Publication date
US7993784B2 (en) 2011-08-09
US7842424B2 (en) 2010-11-30
DE10147368A1 (en) 2002-04-25
US20050048332A1 (en) 2005-03-03
JP2002198074A (en) 2002-07-12
US20050048333A1 (en) 2005-03-03

Similar Documents

Publication Publication Date Title
US7081312B1 (en) Multiple stage combustion process to maintain a controllable reformation temperature profile
JP4340315B2 (en) FUEL CELL POWER PLANT AND METHOD OF OPERATING FUEL CELL POWER PLANT
US8231697B2 (en) Rapid start fuel reforming systems and techniques
US8062799B2 (en) High-efficiency dual-stack molten carbonate fuel cell system
US7270901B2 (en) Combined autothermal/steam reforming fuel processor mechanization
US6312842B1 (en) Water retention system for a fuel cell power plant
KR100286572B1 (en) Fuel cell vehicle small fuel reformer and its system using metal thin film
EP1241723B1 (en) Water recovery for a fuel cell system
US7338727B2 (en) Method of operating a fuel cell to provide a heated and humidified oxidant
JP4065235B2 (en) Water vapor transfer device for fuel cell reformer
US6277509B1 (en) Hydride bed water recovery system for a fuel cell power plant
JPH06314570A (en) Fuel cell manifold structure

Legal Events

Date Code Title Description
AS Assignment

Owner name: GENERAL MOTORS CORPORATION, MICHIGAN

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:PETTIT, WILLIAM HENRY;REEL/FRAME:011182/0679

Effective date: 20000919

STCF Information on status: patent grant

Free format text: PATENTED CASE

AS Assignment

Owner name: GM GLOBAL TECHNOLOGY OPERATIONS, INC., MICHIGAN

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:GENERAL MOTORS CORPORATION;REEL/FRAME:022092/0737

Effective date: 20050119

Owner name: GM GLOBAL TECHNOLOGY OPERATIONS, INC.,MICHIGAN

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:GENERAL MOTORS CORPORATION;REEL/FRAME:022092/0737

Effective date: 20050119

AS Assignment

Owner name: UNITED STATES DEPARTMENT OF THE TREASURY, DISTRICT

Free format text: SECURITY AGREEMENT;ASSIGNOR:GM GLOBAL TECHNOLOGY OPERATIONS, INC.;REEL/FRAME:022201/0501

Effective date: 20081231

AS Assignment

Owner name: CITICORP USA, INC. AS AGENT FOR BANK PRIORITY SECU

Free format text: SECURITY AGREEMENT;ASSIGNOR:GM GLOBAL TECHNOLOGY OPERATIONS, INC.;REEL/FRAME:022556/0013

Effective date: 20090409

Owner name: CITICORP USA, INC. AS AGENT FOR HEDGE PRIORITY SEC

Free format text: SECURITY AGREEMENT;ASSIGNOR:GM GLOBAL TECHNOLOGY OPERATIONS, INC.;REEL/FRAME:022556/0013

Effective date: 20090409

AS Assignment

Owner name: GM GLOBAL TECHNOLOGY OPERATIONS, INC., MICHIGAN

Free format text: RELEASE BY SECURED PARTY;ASSIGNOR:UNITED STATES DEPARTMENT OF THE TREASURY;REEL/FRAME:023238/0015

Effective date: 20090709

XAS Not any more in us assignment database

Free format text: RELEASE BY SECURED PARTY;ASSIGNOR:UNITED STATES DEPARTMENT OF THE TREASURY;REEL/FRAME:023124/0383

AS Assignment

Owner name: GM GLOBAL TECHNOLOGY OPERATIONS, INC., MICHIGAN

Free format text: RELEASE BY SECURED PARTY;ASSIGNORS:CITICORP USA, INC. AS AGENT FOR BANK PRIORITY SECURED PARTIES;CITICORP USA, INC. AS AGENT FOR HEDGE PRIORITY SECURED PARTIES;REEL/FRAME:023127/0326

Effective date: 20090814

AS Assignment

Owner name: UNITED STATES DEPARTMENT OF THE TREASURY, DISTRICT

Free format text: SECURITY AGREEMENT;ASSIGNOR:GM GLOBAL TECHNOLOGY OPERATIONS, INC.;REEL/FRAME:023155/0922

Effective date: 20090710

AS Assignment

Owner name: UAW RETIREE MEDICAL BENEFITS TRUST, MICHIGAN

Free format text: SECURITY AGREEMENT;ASSIGNOR:GM GLOBAL TECHNOLOGY OPERATIONS, INC.;REEL/FRAME:023161/0864

Effective date: 20090710

FPAY Fee payment

Year of fee payment: 4

AS Assignment

Owner name: GM GLOBAL TECHNOLOGY OPERATIONS, INC., MICHIGAN

Free format text: RELEASE BY SECURED PARTY;ASSIGNOR:UAW RETIREE MEDICAL BENEFITS TRUST;REEL/FRAME:025311/0680

Effective date: 20101026

Owner name: GM GLOBAL TECHNOLOGY OPERATIONS, INC., MICHIGAN

Free format text: RELEASE BY SECURED PARTY;ASSIGNOR:UNITED STATES DEPARTMENT OF THE TREASURY;REEL/FRAME:025245/0273

Effective date: 20100420

AS Assignment

Owner name: WILMINGTON TRUST COMPANY, DELAWARE

Free format text: SECURITY AGREEMENT;ASSIGNOR:GM GLOBAL TECHNOLOGY OPERATIONS, INC.;REEL/FRAME:025327/0222

Effective date: 20101027

AS Assignment

Owner name: GM GLOBAL TECHNOLOGY OPERATIONS LLC, MICHIGAN

Free format text: CHANGE OF NAME;ASSIGNOR:GM GLOBAL TECHNOLOGY OPERATIONS, INC.;REEL/FRAME:025780/0795

Effective date: 20101202

FPAY Fee payment

Year of fee payment: 8

AS Assignment

Owner name: GM GLOBAL TECHNOLOGY OPERATIONS LLC, MICHIGAN

Free format text: RELEASE BY SECURED PARTY;ASSIGNOR:WILMINGTON TRUST COMPANY;REEL/FRAME:034183/0680

Effective date: 20141017

MAFP Maintenance fee payment

Free format text: PAYMENT OF MAINTENANCE FEE, 12TH YEAR, LARGE ENTITY (ORIGINAL EVENT CODE: M1553)

Year of fee payment: 12